CN113440884B

CN113440884B - Tower set temperature self-adaptive adjusting method, system and storage medium

Info

Publication number: CN113440884B
Application number: CN202110763038.4A
Authority: CN
Inventors: 杨自中; 王浩; 王文博; 王远辉; 张宏科
Original assignee: Wanhua Chemical Group Co Ltd; Wanhua Chemical Ningbo Co Ltd
Current assignee: Wanhua Chemical Group Co Ltd; Wanhua Chemical Ningbo Co Ltd
Priority date: 2021-07-06
Filing date: 2021-07-06
Publication date: 2022-09-20
Anticipated expiration: 2041-07-06
Also published as: CN113440884A

Abstract

The application discloses a tower group temperature self-adaptive adjusting method, a system and a storage medium, which are used for realizing self-adaptive adjustment of the temperature of each tower in a tower group and reducing the workload of operators. The method comprises the following steps: determining the feeding flow of each tower in the tower group in the operation process of the tower group; judging whether a first target tower with changed feeding flow exists or not; when a first target tower with changed feeding flow exists, determining the temperature corresponding to the first target tower according to the feeding flow of the first target tower; and adjusting the steam flow of the first target tower according to the temperature corresponding to the first target tower so as to adjust the current temperature of the first target tower to the temperature corresponding to the first target tower. By adopting the scheme provided by the application, the self-adaptive adjustment of the temperature of each tower in the tower group is realized, the workload of operators is reduced, and the labor cost is saved.

Description

Tower set temperature self-adaptive adjusting method, system and storage medium

Technical Field

The present application relates to the field of internet technologies, and in particular, to a tower temperature adaptive adjustment method, system, and storage medium.

Background

The rectifying tower is a tower-type gas-liquid contact device for rectifying. The light component in the liquid phase is transferred to the gas phase, and the heavy component in the gas phase is transferred to the liquid phase by utilizing the property that each component in the mixture has different volatility, namely, the vapor pressure of each component is different at the same temperature, so that the aim of separation is fulfilled. The rectifying tower is also a mass and heat transfer device which is widely applied in petrochemical production.

At present, in order to realize good separation effect of multiple components, a tower group formed by connecting a plurality of rectifying towers in series can be adopted for rectification. In the prior art, only a scheme for controlling the temperature of a single tower exists, a scheme for controlling the temperature of a tower group formed by connecting a plurality of towers in series does not exist, and an operator is also required to perform manual adjustment in the scheme for controlling the temperature of the single tower, so that how to achieve self-adaptive adjustment of the temperature of each tower in the tower group and reduce the workload of the operator is an urgent technical scheme.

Disclosure of Invention

The application provides a tower group temperature self-adaptive adjusting method, a tower group temperature self-adaptive adjusting system and a storage medium, which are used for realizing self-adaptive adjustment of the temperature of each tower in a tower group and reducing the workload of operators.

The application provides a tower group temperature self-adaptive adjusting method, which comprises the following steps:

determining the feeding flow of each tower in the tower group in the operation process of the tower group;

judging whether a first target tower with changed feeding flow exists or not;

when a first target tower with changed feeding flow exists, determining the temperature corresponding to the first target tower according to the feeding flow of the first target tower;

and adjusting the steam flow of the first target tower according to the temperature corresponding to the first target tower so as to adjust the current temperature of the first target tower to the temperature corresponding to the first target tower.

The beneficial effect of this application lies in: in the operation process of the tower set, the feeding flow of each tower in the tower set is determined, and when a first target tower with the changed feeding flow exists, the steam flow of the first target tower is adjusted to adjust the current temperature of the first target tower to the temperature corresponding to the first target tower, so that the self-adaptive adjustment of the temperature of each tower in the tower set is realized, the workload of operators is reduced, and the labor cost is saved.

In one embodiment, further comprising:

determining liquid level information of each tower in the tower group in the operation process of the tower group;

determining the importance of liquid level control of each tower in the group according to the liquid level information;

when a second target tower with the variable liquid level control importance exists, adjusting the feeding flow and the extraction flow of the second target tower to reduce the liquid level control importance of the second target tower;

determining the temperature corresponding to the second target tower according to the adjusted feeding flow of the second target tower;

and adjusting the steam flow of the second target tower according to the temperature corresponding to the second target tower so as to adjust the current temperature of the second target tower to the temperature corresponding to the second target tower.

The beneficial effect of this embodiment lies in: in the operation process of the tower set, the liquid level information of each tower in the tower set can be determined; determining the importance of liquid level control of each tower in the group according to the liquid level information; when a second target tower with the variable liquid level control importance exists, adjusting the feeding flow and the extraction flow of the second target tower to reduce the liquid level control importance of the second target tower; therefore, the self-adaptive adjustment of the liquid level of each tower in the tower set is realized, the workload of operators is reduced, and the labor cost is saved.

In one embodiment, determining the importance of real-time level control for each column in the stack based on the level information comprises:

determining the importance degree Ia of each tower;

determining the control importance degree Is of the liquid level of each tower;

and determining the control importance I of the liquid level of each tower according to the importance Ia of each tower and the control importance Is of the liquid level of each tower.

In one embodiment, the determining the importance level Ia of each tower comprises:

if Lmax is larger than Lr and larger than Lmin, Ia is 0 when t is larger than or equal to 1/3 or t is smaller than 0, and Ia is 1/t when t is larger than or equal to 0 and smaller than 1/3;

if L is more than or equal to Lmax, Ia is 3+ (L-Lmax) 100/5;

if L is less than or equal to Lmin, Ia is 3+ (Lmin-L) 100/5;

wherein t is the duration of the current liquid level, and is calculated by the following formula:

t＝(Lr*V)/(Fout-Fin*α_btm)；

wherein Lr is a tolerance value of the liquid level; v is the volume of the column; fout is the production flow; fin is the feed flow; l is the actual value of the liquid level; lmax is the upper limit of liquid level tolerance; lmin is the lower limit of liquid level tolerance; alpha _ btm is a feeding coefficient extracted from a tower kettle;

lr is calculated as follows: if Lr > (Lmax + Lmin)/2, then Lr is L-Lmax; if Lr is less than or equal to (Lmax + Lmin)/2, then Lr is L-Lmin.

In one embodiment, the determining the control importance Is of each column level comprises:

inputting the liquid level deviation eL and the liquid level change rate ecL of each tower into a fuzzy controller as real quantity values of each tower;

acquiring the control importance degree Is of the fuzzy controller for determining the liquid level of each tower based on the real quantity value;

and the fuzzy controller determines the control importance degree Is of each tower liquid level based on the real quantity value in the following way:

converting the real quantity value of each tower into fuzzy quantity described by natural language, wherein the range of a real quantity value discourse domain U of the liquid level deviation is [ -3, 3], a corresponding fuzzy set of the natural language discourse domain U is { NB, NS, ZO, PS, PB }, and the subset elements are respectively negative big, negative small, zero, positive small and positive big; the range of a real-quantity value discourse domain U of the liquid level change rate ecL is [ -3, 3], a corresponding natural language discourse domain U fuzzy set is { SB, SS, ZO, FS, FB }, and subset elements are respectively negative fast, negative slow, zero, positive slow and positive fast; and determining the control importance degree Is of the liquid level of each tower according to the subset elements corresponding to the real quantity values of each tower.

In one embodiment, the determining the importance of control of the liquid level I of each column according to the importance Ia of each column and the importance of control of the liquid level Is of each column includes:

determining the importance I of the liquid level control of each tower according to the following formula:

I＝0.4Ia+0.1Is；

wherein Ia is the importance of each column; is the degree of importance in the control of the liquid level in each column.

In one embodiment, the determining the feed flow rate to each column within the column group comprises:

the feed flow to each column in the column group is determined by the following equation:

Fin＝Pb+Qb+Fm+F0；

wherein Fin is the feeding flow of each tower (the same as the upper tower extraction flow corresponding to each tower); pb is a change value of the PID control action of the upper tower; qb is the feed-forward action change value of the upper tower; fm is a lower tower feedback effect change value; f0 is the raw feed flow rate of each column.

In one embodiment, said determining the temperature corresponding to said first target column based on the feed flow rate to said first target column comprises:

determining the temperature corresponding to the first target tower according to the following formula:

T＝K(F _{_feed2} -F _{_feed1} )+Tlast

wherein T is a temperature determined according to the feed flow rate; k is a temperature corresponding coefficient of the feeding tower; f _ feed1 is an initial value of the feed flow within a preset sampling time (namely the feed flow before change); f _ feed2 is the final value of the feed flow within the preset sampling time (i.e. the feed flow after the change); tlast is the column temperature set point at feed flow rate F feed 1.

The application also provides a tower group temperature self-adaptive adjustment system, including:

at least one processor; and the number of the first and second groups,

a memory communicatively coupled to the at least one processor; wherein,

the memory stores instructions executable by the processor to implement the tower temperature adaptive adjustment method described in any of the above embodiments.

The present application also provides a computer-readable storage medium, wherein when instructions in the storage medium are executed by a processor corresponding to the tower group temperature adaptive adjustment system, the tower group temperature adaptive adjustment system is enabled to implement the tower group temperature adaptive adjustment method described in any of the above embodiments.

Additional features and advantages of the application will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by the practice of the application. The objectives and other advantages of the application may be realized and attained by the structure particularly pointed out in the written description and claims hereof as well as the appended drawings.

The technical solution of the present application is further described in detail by the accompanying drawings and examples.

Drawings

The accompanying drawings are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate embodiment(s) of the application and together with the description serve to explain the application and not limit the application. In the drawings:

FIG. 1 is a flow chart of a method for adaptively adjusting tower group temperature according to an embodiment of the present application;

FIG. 2 is a flow chart of a method for adaptive tower group temperature regulation according to another embodiment of the present application;

FIG. 3 is a flow chart of a method for adaptively adjusting tower group temperature according to another embodiment of the present application;

FIG. 4 is a schematic view of a connection between two towers of a tower set according to an embodiment of the present application;

fig. 5 is a schematic diagram of a hardware structure of a tower temperature adaptive adjustment system according to the present application.

Detailed Description

The preferred embodiments of the present application will be described in conjunction with the accompanying drawings, and it will be understood that they are described herein only to illustrate and explain the present application and not to limit the present application.

Fig. 1 is a flowchart of an adaptive tower temperature adjustment method according to an embodiment of the present application, and as shown in fig. 1, the method may be implemented as the following steps S11-S14:

in step S11, during operation of the column stack, determining the feed flow rate to each column within the column stack;

in step S12, it is determined whether or not there is a first target column in which the feed flow rate is changed;

in step S13, when there is a first target column with a changed feed flow rate, determining a temperature corresponding to the first target column according to the feed flow rate of the first target column;

in step S14, the steam flow of the first target column is adjusted according to the temperature corresponding to the first target column, so as to adjust the current temperature of the first target column to the temperature corresponding to the first target column.

In this application, at the tower group operation in-process, can detect the charge flow of tower, under the condition that charge flow changes, adjust the temperature of tower. In order to reduce process fluctuation, the liquid level and the temperature of each tower need to be stably controlled as much as possible, but the fluctuation of the temperature and the liquid level of each tower is often accompanied with a plurality of operations when the load is adjusted, the temperature of each tower is also usually adjusted because of the requirement of separation effect, and the liquid level of a certain tower can greatly fluctuate when special conditions occur, the liquid level of the tower can not be adjusted well, the circulating fluctuation of the liquid level and the temperature of the front tower and the rear tower can be caused, and the operation amount is large. That is, the present application will adaptively adjust the liquid level in addition to the temperature of the column. Thereby reducing process fluctuations.

Specifically, in this application, when the rectifying tower set is in operation, the liquid level change and the flow change are monitored: the feed flow rate can be changed when the feed is disturbed or the material source is insufficient. Changes in feed flow rate can cause the subject of the present application (e.g., the adaptive conditioning system associated with the column set) to perform temperature conditioning; meanwhile, the liquid level of the tower can be changed due to the change of the feeding flow, and if the liquid level is changed and operated in a specified interval, the feeding flow of the tower and the adjacent front and rear towers can be adjusted by the execution main body in order to enable the liquid level of the tower to return to the specified interval as soon as possible. Thus, if the liquid level exceeds the interval, the feed flow rate will change, and the temperature change will continue to be caused. That is, changes in feed flow rate can cause changes in temperature and liquid level, which can also cause changes in feed flow rate.

Thus, in the present application, during operation of the column stack, the feed flow rate to each column within the column stack is determined; the feed flow rate of each column changes, and the reasons for the changes are mentioned above, that is, there are flow rate changes due to feed disturbance, flow rate changes due to insufficient material source, flow rate changes due to adjustment of the flow rates of the column and the adjacent columns in the column group in order to return the liquid level of the column to a predetermined interval as soon as possible, and the like. Judging whether a first target tower with changed feeding flow exists or not; when a first target tower with changed feeding flow exists, determining the temperature corresponding to the first target tower according to the feeding flow of the first target tower; and adjusting the steam flow of the first target tower according to the temperature corresponding to the first target tower so as to adjust the current temperature of the first target tower to the temperature corresponding to the first target tower.

Secondly, in the application, in the operation process of the tower set, the liquid level information of each tower in the tower set is determined; determining the importance of liquid level control of each tower in the group according to the liquid level information; when a second target tower with the variable liquid level control importance exists, adjusting the feeding flow and the extraction flow of the second target tower to reduce the liquid level control importance of the second target tower; determining the temperature corresponding to the second target tower according to the adjusted feeding flow of the second target tower; and adjusting the steam flow of the second target tower according to the temperature corresponding to the second target tower so as to adjust the current temperature of the second target tower to the temperature corresponding to the second target tower.

It will be appreciated that secondly, because the feed flow has a feed forward effect, if the feed flow changes, it will also cause the feed flow to each column following the main body of the subject application to be adjusted. In addition, when the liquid level of the second target column exceeds the prescribed interval, in order to return the liquid level of the second target column to the prescribed interval as soon as possible, the execution main body adjusts the feed flow rates of the second target column and the adjacent preceding and succeeding columns, and therefore, the feed flow rate of the second target column also changes, and therefore, the second target column and the first target column may be the same column.

In the application, when the real-time liquid level control importance of each tower in the group is determined according to the liquid level information, the importance degree Ia of each tower is determined; determining the control importance degree Is of the liquid level of each tower; and determining the control importance I of the liquid level of each tower according to the importance Ia of each tower and the control importance Is of the liquid level of each tower.

Wherein, determining the importance level Ia of each tower comprises:

if L is more than or equal to Lmax, Ia is 3+ (L-Lmax) 100/5;

if L is less than or equal to Lmin, Ia is 3+ (Lmin-L) 100/5;

t＝(Lr*V)/(Fout-Fin*α_btm)；

Determining the control importance degree Is of each tower liquid level, comprising:

the deviation eL between the actual and the set value of the liquid level of each column is defined as:

eL＝L-L ^*

in the formula: l is the actual value of the liquid level of each column, L ^* Is the set value of the liquid level of each tower;

the rate of change of liquid level ecL for each column is defined as:

acquiring a control importance degree Is of the liquid level of each tower determined by the fuzzy controller based on the real quantity value;

the mode that the fuzzy controller determines the control importance degree Is of each tower liquid level based on the real quantity value Is as follows:

converting the real quantity value of each tower into fuzzy quantity described by natural language, wherein the range of a real quantity value discourse domain U of the liquid level deviation is [ -3, 3], a corresponding fuzzy set of the natural language discourse domain U is { NB, NS, ZO, PS, PB }, and the subset elements are respectively negative big, negative small, zero, positive small and positive big; the range of a real-quantity value discourse domain U of the liquid level change rate ecL is [ -3, 3], a corresponding natural language discourse domain U fuzzy set is { SB, SS, ZO, FS, FB }, and subset elements are respectively negative fast, negative slow, zero, positive slow and positive fast;

determining the control importance degree Is of the liquid level of each tower according to the subset elements corresponding to the real quantity values of each tower, specifically determining the importance degree Is of the liquid level of each tower according to the following table 1:

TABLE 1

For example, if the liquid level deviation eL of a certain column Is 5% (corresponding to PS) and the liquid level change rate ecL Is 0 (corresponding to Z0), the single-column liquid level importance Is 1.

Determining the control importance I of the liquid level of each tower according to the importance Ia of each tower and the control importance Is of the liquid level of each tower, wherein the control importance I comprises the following steps: determining the importance I of the liquid level control of each tower according to the following formula:

I＝0.4Ia+0.1Is；

Determining feed flow rates to each column in the column group, comprising:

Fin＝Pb+Qb+Fm+F0；

Wherein, the change value Pb of the PID control action of the upper tower is determined according to the following modes:

the difference eI between the importance of the liquid level of the tower and the liquid level of the upper tower and the deviation eL of the liquid level of the tower are used as real values and input into a fuzzy controller. The fuzzy rule of the fuzzy controller is shown in the following table 2, and the fuzzy subset of the input variable eI is: when the deviation value eI is greater than 0, the importance of the liquid level of the tower at the moment is higher than that of the liquid level of the upper tower at the moment, and the state is defined as high; when the deviation value e is less than 0, the importance of the liquid level of the tower is lower than that of the upper tower at the moment, and the state is defined as low; when the deviation e is 0, the liquid level importance is equal to that of the upper column, and this state is defined as equal. The fuzzy subset of the input variable eL is defined as high _ liqid level when the liquid level deviation is more than 10; when the liquid level deviation is 0-10, defining the liquid level deviation as normal _ liqid level; and when the liquid level deviation change rate is-10-0, defining the liquid level deviation change rate as normal _ liqid level, and when the liquid level deviation is less than-10, defining the liquid level deviation change rate as low _ liqid level. The fuzzy subset corresponding to the output variable U is { OF, OM, OS, CS, CM, CF }, and each variable in the subset represents a fixed PID parameter.

TABLE 2

According to

And calculating PID action regulating quantity, wherein e is deviation, Kp, Td and Ts are all regulating parameters, and t is time. Kp, Td, Ts are obtained by a step response method.

Determining the change value Fm of the tower feedback effect: if eI is greater than 0, the lower tower feedback effect variation value Fm is k eI, and if eI is less than 0, the lower tower feedback effect variation value is 0.

k is the corresponding coefficient of the feeding material and the liquid level of the tower, and is determined by the following formula:

wherein: fout is the feed flow of the tower; v is the volume of the column.

The above-mentioned upper tower feed-forward action variation value Qb is determined by the following formula:

Qb＝(F_feed2-F_feed1)×α_btm

wherein: f _ feed1 is the initial value of the feed flow in the preset sampling time; f _ feed2 is the final value of the feed flow within a preset sampling time; α _ btm represents the column bottom draw feed coefficient.

The column bottom withdrawal feed coefficient α _ btm is determined by the following equation:

wherein: f _ feed11 is an initial value of the feed flow in a preset sampling time when the liquid level and the feed flow are stable before load adjustment; f _ feed21 is the final value of the feed flow in the preset sampling time when the liquid level and the feed flow are stable before the load adjustment; b _ btm1 is an initial value of the tower kettle flow rate in a preset sampling time when the liquid level and the feed flow rate are stable before load adjustment; and the final value of the tower kettle extraction flow within the preset sampling time when the liquid level and the feed flow are stable before the B _ btm2 load is adjusted.

The temperature corresponding to the first target column is determined according to the feeding flow of the first target column, and the temperature corresponding to the second target column is determined according to the adjusted feeding flow of the second target column, which are determined by the following formulas:

T＝K(F _{_feed2} -F _{_feed1} )+Tlast

wherein T is a temperature determined according to the feed flow rate; k is the temperature corresponding coefficient of the feeding tower; f _ feed1 is the initial value of the feed flow within the preset sampling time (i.e. the feed flow before the change occurs); f _ feed2 is the final value of the feed flow within the preset sampling time (i.e. the feed flow after the change); tlast is the column temperature set point at feed flow rate F feed 1.

Specifically, after the temperature is determined, the steam flow of the tower needs to be adjusted according to the determined temperature, and the steam flow is determined by the following method:

Fz＝Pz+Qz+Lz+Fz0

wherein Fz is the steam flow of each tower (equal to the steam flow extracted from the upper tower); pz is a temperature PID control action change value; qz is the feed effect variation value; lz is the change value of the liquid level action of the tower; fz0 is the original steam flow of each tower;

and determining the PID control action of the temperature according to the deviation of the actual temperature value and the set value. Specifically, the temperature PID action variation value is calculated according to the following formula:

wherein e is deviation, Kp, Td and Ts are all adjusting parameters, and t is time. Kp, Td, Ts are obtained by a step response method.

Multiplying the change value of the tower feeding flow in a specific time by a steam heat flow conversion coefficient to obtain a feedforward value for regulating the steam flow of the tower kettle of the separation tower; when the change value of the tower feeding flow in a specific time is stable, the steam heat flow conversion coefficient of the tower kettle steam flow regulation is corrected and calculated to obtain the continuously corrected steam heat flow conversion coefficient. The method specifically comprises the following steps:

Qz＝(F_feed2-F_feed1)×α_vapor

wherein Qz is a feed effect variation value; f _ feed1 is the initial value of the feed flow in the preset sampling time; f _ feed2 is the final value of the feed flow within a preset sampling time; and alpha _ vapor is a steam flow conversion coefficient.

The steam heat flow conversion coefficient is determined by adopting the following method:

the F _ feed11 is an initial value of the feeding flow within a preset sampling time when the temperature and the feeding flow are stable before load adjustment; f _ feed21 is the final value of the feed flow within the preset sampling time when the temperature and the feed flow are stable before load adjustment; b _ vapor11 is the initial value of the steam flow within the preset sampling time when the temperature and the feed flow are stable before the load adjustment; b _ vapor21 final steam flow value at preset sample time when temperature and feed flow stabilized before load adjustment.

In addition, the liquid level change of the tower can also cause the temperature change of the tower, so the influence of the liquid level change of the tower on the steam is tested in a step mode to obtain the relation of the liquid level change to the steam:

Lz＝(L_2-L_1)×α_LT

wherein, Lz is the change value of the liquid level action of the tower; l _1 is an initial value of the tower liquid level within a preset sampling time; l _2 is the final value of the tower liquid level within the preset sampling time; α _ LT is a liquid level vapor conversion factor, wherein the liquid level vapor conversion factor is determined using the following method:

wherein L is ₁₁ The initial value of the liquid level of the tower kettle in the preset sampling time of the tower is obtained; l is ₂₁ The final value of the liquid level of the tower kettle in the preset sampling time of the tower is obtained; b _ vapor11 is the initial value of the steam flow of the tower in the preset sampling time; b _ vapor21 final steam flow for preset sample time.

The temperature, the feeding flow and the steam of each tower in the tower group can be determined as much as possible through the formula, and then the temperature, the feeding flow and the steam flow of each tower can be issued to the control host corresponding to each tower, so that each control host controls the feeding flow, the temperature and the steam flow of each tower.

Through the above, the temperature control and liquid level control of each column in the rectifying column group are explained by combining with specific formulas. The following detailed exemplary description of the control of temperature control and liquid level control of each column in a rectification column stack in this application is given by way of example in conjunction with the above equations:

the connection mode of the tower group is shown in fig. 4, fig. 4 is a schematic connection relation diagram of two towers in the tower group, wherein each reference number in the tower 4 has the following meaning:

feed-forward action of feed flow of an X tower on extraction flow; the liquid level of the X tower plays a role in PID control of the produced flow; the feedback effect of the liquid level of the X +1 tower on the extraction flow of the X tower; feed-forward action of X tower feeding flow to steam flow; the liquid level of the X tower acts on the steam flow; sixthly, PID action of the temperature of the X tower on the steam flow; seventhly, the feed flow of the tower X +1 has a feed-forward effect on the extraction flow; controlling PID of the liquid level of the tower X +1 on the extracted flow; the liquid level of the tower ninthly-X +2 has a feedback effect on the output flow of the tower X + 1; feed forward effect of feed flow to column r-X +1 on steam flow;

-effect of X +1 column liquid level on steam flow;

-PID effect of X +1 column temperature on steam flow;

the feedback effect of the liquid level of the X tower on the extraction flow of the X-1 tower is realized;

-the flow from the column X-1;

-the flow to the column X + 2;

a certain synthesis unit (such as petroleum) is used for separating impurities and purifying products by a continuous rectification system, the separation effect of each tower needs to be ensured, the liquid level is controlled as much as possible to be stable, and the influence on the downstream is reduced. Wherein the upper and lower limits of the liquid level control of the tower 1 are 70% and 30%, the upper and lower limits of the liquid level control of the tower 2 are 80% and 40%, the upper and lower limits of the liquid level control of the tower 3 are 80% and 40%, and the size of each tower is 100m ³ 、120m ³ 、120m ³ . The feed flow rates of the columns 1, 2 and 3 in a stable condition were 240m respectively ³ /h，192m ³ /h，153.6m ³ H is used as the reference value. The temperature of each column was controlled at 182 deg.C, 183 deg.C and 183.2 deg.C, respectively.

The invention is explained for different situations:

(1) when the load is stable

1. The liquid levels of the towers 2 and 3 are respectively about 50%, 60% and 60% in a control interval, the temperature Is also controlled stably, the liquid level change rate and the liquid level deviation are both 0, the single-tower liquid level importance Is1 Is2 Is3 Is 0, and the method Is characterized in that

It is understood that t1, t2, and t3 are infinite, and Ia1 ═ Ia2 ═ Ia3 ═ 0, and that the liquid level importance I of each column is 0, that is, the liquid level importance of the three columns is the same.

1. The feed flow rates of the 2 and 3 columns were 240m, respectively ³ /h，192m ³ /h，153.6m ³ H is used as the reference value. The tower 1 feedback coefficient is-2.4 h, the tower 2 feedback coefficient is-1.6 h, the tower 3 feedback coefficient is-1.28 h, the tower 1 feedforward coefficient is 0.8, the tower 2 feedforward coefficient is 0.8, and the tower 3 feedforward coefficient is 0.8. The change in column feed effect Qb is 0 and the change in column PID effect Pb is 0. When the feedback variation fb of each column is 0, the take-off flow of each column is constant, i.e., the feed flow of each column 1, 2, or 3 is 240m ³ /h，192m ³ /h，153.6m ³ /h。

When the set value of each column temperature is not changed, the feed action Qz of each column is 0, the PID action Pz of each column is 0, and the liquid level action Lz of each column is 0, the steam flow rate of each column is not changed. The liquid level and the temperature of each tower are continuously controlled within the target range to meet the control requirement.

(2)1 tower feed flow is reduced, 2 tower and 3 tower are normal

1 column feed from 240m ³ The reduction of/h is 190m ³ The liquid levels of the towers 1, 2 and 3 are all in a set interval at the beginning, the liquid levels are respectively about 50 percent, 60 percent and 60 percent, and the feeding flow rates of the towers 1, 2 and 3 are respectively 190m ³ /h，192m ³ /h，153.6m ³ H is used as the reference value. By

Thus, Fin1 ═ 190m ³ /h，Fout1＝192m ³ /h，Fout2＝153.6m ³ /h，Fout3＝122.88m ³ If t1 Is 0.5h, t2 and t3 are infinite, Ia1 Is 0, Ia2 Is Ia3 Is 0, and the liquid level change rate and the liquid level deviation are 0, the liquid level importance of the single tower Is1 Is2 Is3 Is 0, I Is 0, that Is, the liquid level importance of the three towers Is the same. The liquid level change rate and the liquid level deviation of each tower are both 0, and the feed-forward action value of 1 tower is-40 m ³ H, the PID action value of 1 tower is 0, and the feedback action change value of 1 tower is 0m ³ H, the production flow of the 1 tower is 152m ³ H; 2 tower feed forward action value-32 m ³ H, the PID action value of the 2 tower is 0, the feedback action change value of the 2 tower is 0m3/h, and the extraction flow of the 2 tower is 121.6m ³ H; feed forward action value of 3 tower-25.6 m ³ H, the PID action value of the 3 towers is 0, the change value of the feedback action of the 3 towers is 0, and the extraction flow of the 3 towers is 102.4m ³ /h。

The liquid levels of the towers 1, 2 and 3 are in a set interval in the circulation, the liquid levels are respectively about 50 percent, 60 percent and 60 percent, and the feeding flow rates of the towers 1, 2 and 3 are respectively 190m ³ /h，152m ³ /h，121.6m ³ H is used as the reference value. By

Then Fout-Fin × btm Is 0, t1, t2, and t3 are all infinite, Ia1 Is Ia2 Is Ia3 Is 0, the liquid level change rate and the liquid level deviation are both 0, the single-tower liquid level importance Is1 Is2 Is3 Is 0, and I Is 0, that Is, the liquid level importance of the three towers Is the same. The production flow of each tower is unchanged.

Since the feed rates of the columns 1, 2 and 3 became 190m, respectively ³ /h，152m ³ /h，121.6m ³ The temperature set value of the tower 1 is gradually and automatically adjusted to 181 ℃, the feeding action Qz1 of the tower 1 is-40 × 50 to-2000 kg/h, the PID action value Pz1 of the tower 1 is less than 0, the liquid level action value Lz1 of the tower 1 is 0, the steam flow of the tower 1 is reduced to-2000 + Pz1, the temperature is gradually reduced, the PID action value Pz is gradually reduced until the temperature of the tower is adjusted to 181 ℃, and the Pz tends to 0; the set value of the 2-tower temperature is gradually and automatically adjusted to 182.5 ℃, the feeding action Qz of the 2-tower is-32 x 55-1760 kg/h, the liquid level action Lz2 of the 2-tower is 0, the PID action value Pz2 of the 2-tower is less than 0, the steam flow of the 2-tower is reduced to-1760 + Pz2, the temperature of the 2-tower is gradually reduced, the PID action value Pz2 is gradually reduced until the tower temperature is adjusted to 182.5 ℃, and the Pz2 tends to 0; the 3-tower temperature set value is gradually and automatically adjusted to 182.6 ℃, the 3-tower feeding action Qz is-24, 54 and-1296 kg/h, the 3-tower liquid level action Lz3 is 0, the 3-tower PID action value Pz3 is less than 0, the 3-tower steam flow is reduced to-1296 + Pz3, the 3-tower temperature is gradually reduced, the PID action value Pz3 is gradually reduced until the tower temperature is adjusted to 182.6 ℃, and the Pz3 approaches 0. The liquid level and the temperature of each tower are gradually adjusted and controlled within a target range to meet the control requirement.

(3) Normal in tower 1, increased in liquid level in tower 2 and normal in tower 3

The feeding of the tower 1 is normal, the liquid level of the tower 2 is increased to 80% due to one strand of interference feeding, the upper limit of a tolerance interval is reached, the liquid level needs to be quickly reduced, the liquid levels of the tower 1 and the tower 3 are initially in a set interval and are respectively about 50% and 60%, and the feeding flow rates of the tower 1, the tower 2 and the tower 3 are respectively 240m ³ /h、192m ³ /h、153.6m ³ H is used as the reference value. The feedback coefficient of 1 tower is-1.6 h. The temperature of each tower Is also controlled stably, the liquid level change rate and the liquid level deviation of 1 tower and 3 towers are both 0, the liquid level importance of a single tower Is 1-Is 3-Is 0, Is 2-Is 4, L2-L2 max, Ia 2-Is 3,

it is understood that t1 and t3 are infinite, and Ia1 equals Ia3 equals 0, so that 1 and 3 liquid level importance I equals 0, and 2-column liquid level importance I2 equals 3 × 0.4+4 × 0.1 equals 1.6.

The liquid level change rate of the tower 1 is 0, and the feed forward action value of the tower 1 is 0m ³ A reaction value of 1 column PID of0, 1 tower feedback variation-1.6-15.36 m ³ H, the production flow of the 1 tower is changed into 176.64m ³ H; 2 tower feed forward action value-12.288 m ³ And h, if the liquid level deviation is high liquid level and the liquid level change rate is high, adopting the strongest PID action to obtain a 2-tower PID action value of 30m ³ 2 tower feedback variation-1.28 (-1.6) 0-0 m ³ H, the production flow of the 2-tower is changed into 171.312m ³ H; feed forward action value of 3 tower 14.17m ³ H, the PID action value of the 3 towers is 0, the change value of the feedback action of the 3 towers is 0, and the extraction flow of the 3 towers is 106.33m ³ /h。

Temperature change: if the feed of the 1 tower is unchanged, the temperature set value of the 1 tower is unchanged, the feed action Qz1 of the 1 tower is 0kg/h, the PID action value Pz1 of the 1 tower is 0, the liquid level action value Lz1 of the 1 tower is 0, and the steam flow of the 1 tower is unchanged; 2 column feed was reduced to 176.64m ³ The temperature set point is automatically gradually reduced to 182.8 ℃, the 2-tower feeding action Qz is-15.36 x 55-844.88 kg/h, the 2-tower liquid level action Lz2 is 20% x 300 is 60kg/h, the 2-tower PID action value Pz2 is less than 0, the 2-tower steam flow is reduced to-784.88 + Pz2, and the 2-tower temperature gradually tends to 182.8 ℃; 3 column feed increase 171.312m ³ And/h, the temperature set value is gradually and automatically adjusted to 183.2 ℃, the 3-tower feeding action Qz3 is 17.712, 54 is 956.448kg/h, the 3-tower liquid level action Lz3 is 0, the 3-tower PID action value Pz3 is more than 0, the 3-tower steam flow is increased by 956.448+ Pz3, the 3-tower temperature is gradually increased to 183.2 ℃, the PID action value Pz3 is gradually reduced until the tower temperature is adjusted to 183.2 ℃, and the Pz3 approaches 0.

After a period of time, the liquid level of the tower 2 is reduced to 60-70 percent, the liquid level of the tower 1 is increased to more than 55 percent, the liquid level of the tower 3 is 60 percent, and the feeding flow rates of the towers 1, 2 and 3 at a certain moment are 240m respectively ³ H, about 190m ³ H, about 170m ³ H is used as the reference value. The tower 1 feedback coefficient is-1.583 h, the tower 2 feedback coefficient is-1.416 h, the tower 1 feedforward coefficient is 0.8, the tower 2 feedforward coefficient is 0.8, and the tower 3 feedforward coefficient is 0.8. The single tower liquid level importance Is1 ═ Is2 ═ Is3 ═ 0, prepared from

It is understood that when t1 is > 2.5h, t2 <0 and t3 is infinite, Ia1 ═ Ia2 ═ Ia3 ═ 0, the liquid level importance I of 1, 2 and 3 columns is equal to 0, i.e., the importance is the same.

Continuously performing cyclic calculation, and setting the subsequent 1 tower feedforward action value as 0m ³ The PID action value of 1 tower is positive, and the feedback action change value of 1 tower is 0m ³ H, the extraction flow of the tower 1 is changed to be more than 190m ³ The flow rate of the liquid in the tower 1 is gradually reduced to 192m ³ H; 2 tower feedforward action value is more than 0m ³ Then gradually reducing to 0, gradually reducing the action value of the 2-tower PID to 0, and changing the value of the 2-tower feedback action to 0m ³ H, the extraction flow of the 2 tower gradually becomes 153.6m ³ H; the feed-forward action value of the 3 towers is gradually reduced, the PID action value of the 3 towers is 0, the change value of the feedback action of the 3 towers is 0, and the recovery flow of the 3 towers is 122.88m ³ /h。

For the temperature, the feeding of the 1 tower is not changed, the temperature set value of the 1 tower is not changed, the feeding action Qz1 of the 1 tower is 0kg/h, the PID action value Pz1 of the 1 tower is 0, and the action value Lz1 of the 1 liquid level is increased along with the liquid level and then gradually reduced to 0; the 2-tower temperature set value is automatically adjusted along with the continuous increase and decrease of feeding, the 2-tower feeding effect is increased and decreased along with the load, the 2-tower liquid level effect Lz2 is gradually reduced to 0, and the 2-tower PID effect value Pz2 is changed along with the temperature deviation until the tower temperature is adjusted to 183 ℃, and Pz2 tends to 0; the 3-tower temperature set value is automatically adjusted gradually along with the increase and decrease of the feeding material, finally, the 3-tower feeding action Qz3 is adjusted back to 183.2 ℃, the 3-tower feeding action Qz3 is increased and decreased along with the load, the 3-tower liquid level action Lz3 is 0, and the 3-tower PID action value Pz3 is changed along with the temperature deviation and finally is 0. Therefore, the liquid level and the temperature of each tower are gradually restored to the normal interval, and the control requirement is met.

According to the above example, the liquid levels and the temperatures of the multiple towers are uniformly controlled, the importance of the liquid levels of the multiple towers is determined through the importance of the liquid level of the single tower and the importance of the tower, the control importance of the liquid level of each tower is further determined, and the priority control of the liquid level of the important tower is realized; the liquid level of the rear tower and the control importance and the production flow of the liquid levels of the front tower and the rear tower are correlated, so that the production of the tower with low liquid level importance level can adjust the liquid level of the tower with high liquid level importance level, namely, the multi-tower liquid level comprehensive control is realized, the fluctuation of the upstream and the downstream is reduced, and the liquid level of the important tower can be quickly adjusted; the liquid level of the tower is related to the steam flow direction, so that the accurate control of the tower temperature is realized. By adopting the method, the time for rapidly restoring each tower to the target liquid level is reduced, and the influence on the downstream is also reduced.

In one embodiment, the method may also be implemented as the following steps A1-A5:

in step A1, determining liquid level information of each tower in the tower group during the operation of the tower group;

in step A2, determining the importance of liquid level control of each tower in the group according to the liquid level information;

in step a4, when there is a second target column with a changed liquid level control importance, adjusting the feed flow and the extraction flow of the second target column to reduce the liquid level control importance of the second target column;

in step A4, determining the temperature corresponding to the second target column according to the adjusted feed flow of the second target column;

in step a5, the steam flow of the second target tower is adjusted according to the temperature corresponding to the second target tower, so as to adjust the current temperature of the second target tower to the temperature corresponding to the second target tower.

In the embodiment, in the operation process of the tower group, the liquid level information of each tower in the tower group is determined; it will be appreciated that the determination of the liquid level information for each column within the column set may be performed simultaneously with the determination of the feed flow rate as described above.

When the tower set runs to a certain time point, the liquid level of the second target tower changes and exceeds the specified interval on the assumption that the feeding flow does not change, so that the importance of the liquid level control of the second target tower can be improved, at the moment, the importance of the liquid level control of the second target tower can be reduced by adjusting the feeding flow and the extraction flow, and the liquid level of the second target tower is reduced to the specified interval.

Since the feed flow rate thereof is also changed, it is necessary to adjust the temperature of the second target column based on the feed flow rate. And after the second target tower has adjusted feed flow and production flow, also can cause the influence to upper tower and lower tower, specifically, because the feed flow of second target tower is equal to the production flow of upper tower, so, at this moment, the upper tower of second target tower is because the change of production flow, and the upper tower liquid level of second target tower also can rise, and when the upper tower liquid level of second target tower rises to surpassing the regulation interval, the liquid level control importance of the upper tower of second target tower also can change to the upper tower that leads to second target tower also can carry out liquid level control, changes its feed flow and production flow promptly. In addition, because the production flow of the second target tower is equal to the feeding flow of the lower tower, the feeding flow of the lower tower is changed to trigger the temperature regulation of the lower tower, and secondly, the change of the feeding flow can also trigger the liquid level regulation of the lower tower along with the time, and so on. It should be noted that the change of the feeding flow rate may be caused by manually adjusting the sizes of the feeding and extraction gates, by the interference of feeding in a certain column, or by the decrease of the feeding flow rate in column 1 due to the shortage of the material source, besides the reason of the liquid level control.

Therefore, as long as the liquid level, the feeding flow or the extraction flow of one tower is changed, the liquid level and the flow of part or all of the towers in the tower group are influenced, and the respective liquid level control or temperature control mechanisms are triggered, so that the dynamic balance can be kept in the operation process of the whole tower group.

From the above description, it is understood that when the above steps S11-S14 and the above steps a1-a5 are performed in combination, one of the execution schemes can be implemented as the following steps B1-B5:

in step B1, during operation of the column group, feed flow information and liquid level information for each column within the column group are determined;

in step B2, determining whether there is a first target column with a changed feed flow rate in the column group according to the feed flow rate information of each column, and determining whether there is a second target column with a changed liquid level control importance in the column group according to the liquid level information of each column, wherein the change in the liquid level control importance is related to the liquid level change;

in step B3, when there is a second target column whose liquid level control importance changes, adjusting the feed flow rate and the withdrawal flow rate of the second target column to reduce the liquid level control importance of the second target column;

in step B4, when there is a first target column with a changed feed flow rate, determining a temperature corresponding to the first target column according to the feed flow rate of the first target column;

in step B5, the steam flow of the first target column is adjusted according to the temperature corresponding to the first target column, so as to adjust the current temperature of the first target column to the temperature corresponding to the first target column.

In one embodiment, as shown in FIG. 2, the above step A2 can be implemented as the following steps S21-S23:

in step S21, the degree of importance Ia of each tower is determined;

in step S22, determining the control importance degree Is of each tower liquid level;

in step S23, the importance of control of each column level I Is determined based on the importance Ia of each column and the importance of control of each column level Is.

In one embodiment, the step S21 includes:

if L is more than or equal to Lmax, Ia is 3+ (L-Lmax) 100/5;

if L is less than or equal to Lmin, Ia is 3+ (Lmin-L) 100/5;

t＝(Lr*V)/(Fout-Fin*α_btm)；

In one embodiment, the above step S22 can be implemented as the following steps S31-S32:

in step S31, the liquid level deviation eL and the liquid level change rate ec of each column are input to the fuzzy controller as actual values of each column;

in step S32, the acquisition fuzzy controller determines the control importance level Is of each tower liquid level based on the real quantity value;

In one embodiment, determining the importance of control of the liquid level of each column I based on the importance of each column Ia and the importance of control of the liquid level of each column Is comprises:

I＝0.4Ia+0.1Is；

In one embodiment, determining the feed flow rate to each column within the column group comprises:

Fin＝Pb+Qb+Fm+F0；

In one embodiment, determining the temperature corresponding to the first target column based on the feed flow rate to the first target column comprises:

T＝K(F _{_feed2} -F _{_feed1} )+Tlast

wherein T is a temperature determined according to the feed flow rate; k is a temperature corresponding coefficient of the feeding tower; f _ feed1 is the initial value of the feed flow within the preset sampling time (i.e. the feed flow before the change occurs); f _ feed2 is the final value of the feed flow within a preset sampling time (i.e. the feed flow after the change); tlast-column temperature set point with feed flow of F _ feed 1.

Fig. 5 is a schematic diagram of a hardware structure of a tower temperature adaptive adjustment system 500 in the present application, including:

at least one processor 502; and the number of the first and second groups,

a memory 504 communicatively coupled to the at least one processor; wherein,

Referring to fig. 5, the tower group temperature adaptive adjustment system 500 may include one or more of the following components: processing component 502, memory 504, power component 506, multimedia component 508, audio component 510, input/output (I/O) interface 512, sensor component 514, and communication component 515.

The processing component 502 generally controls the overall operation of the tower section temperature adaptive tuning system 500. The processing components 502 may include one or more processors 520 to execute instructions to perform all or a portion of the steps of the methods described above. Further, the processing component 502 can include one or more modules that facilitate interaction between the processing component 502 and other components. For example, the processing component 502 can include a multimedia module to facilitate interaction between the multimedia component 508 and the processing component 502.

The memory 504 is configured to store various types of data to support the operation of the system 500 at the tower group temperature. Examples of such data include instructions for any application or method operating on the tower group temperature adaptive tuning system 500, such as text, pictures, video, and the like. The memory 504 may be implemented by any type or combination of volatile or non-volatile memory devices such as Static Random Access Memory (SRAM), electrically erasable programmable read-only memory (EEPROM), erasable programmable read-only memory (EPROM), programmable read-only memory (PROM), read-only memory (ROM), magnetic memory, flash memory, magnetic or optical disks.

The power supply component 506 provides power to the various components of the tower bank temperature adaptive tuning system 500. The power components 506 may include a power management system, one or more power supplies, and other components associated with generating, managing, and distributing power for the tower bank temperature adaptive tuning system 500.

The multimedia components 508 include a screen that provides an output interface between the tower group temperature adaptive tuning system 500 and the user. In some embodiments, the screen may include a Liquid Crystal Display (LCD) and a Touch Panel (TP). If the screen includes a touch panel, the screen may be implemented as a touch screen to receive an input signal from a user. The touch panel includes one or more touch sensors to sense touch, slide, and gestures on the touch panel. The touch sensor may not only sense the boundary of a touch or slide action, but also detect the duration and pressure associated with the touch or slide operation. In some embodiments, the multimedia component 508 may also include a front facing camera and/or a rear facing camera. When the tower temperature adaptive adjustment system 500 is in an operation mode, such as a shooting mode or a video mode, the front camera and/or the rear camera can receive external multimedia data. Each front camera and rear camera may be a fixed optical lens system or have a focal length and optical zoom capability.

The audio component 510 is configured to output and/or input audio signals. For example, the audio component 510 includes a Microphone (MIC) configured to receive an external audio signal when the tower temperature adaptive tuning system 500 is in an operating mode, such as a call mode, a recording mode, and a voice recognition mode. The received audio signal may further be stored in the memory 504 or transmitted via the communication component 515. In some embodiments, audio component 510 further includes a speaker for outputting audio signals.

The I/O interface 512 provides an interface between the processing component 502 and peripheral interface modules, which may be keyboards, click wheels, buttons, etc. These buttons may include, but are not limited to: a home button, a volume button, a start button, and a lock button.

The sensor assembly 514 includes one or more sensors for providing various aspects of condition assessment for the tower section temperature adaptive adjustment system 500. For example, the sensor assembly 514 may include an acoustic sensor. In addition, the sensor component 514 may detect the open/closed state of the tower set temperature adaptive adjustment system 500, the relative positioning of the components, such as the display and keypad of the tower set temperature adaptive adjustment system 500, the sensor component 514 may also detect a change in position of the tower set temperature adaptive adjustment system 500 or a component of the tower set temperature adaptive adjustment system 500, the presence or absence of user contact with the tower set temperature adaptive adjustment system 500, the orientation or acceleration/deceleration of the tower set temperature adaptive adjustment system 500, and a change in temperature of the tower set temperature adaptive adjustment system 500. The sensor assembly 514 may include a proximity sensor configured to detect the presence of a nearby object without any physical contact. The sensor assembly 514 may also include a light sensor, such as a CMOS or CCD image sensor, for use in imaging applications. In some embodiments, the sensor assembly 514 may also include an acceleration sensor, a gyroscope sensor, a magnetic sensor, a pressure sensor, or a temperature sensor.

The communication component 515 is configured to enable the tower temperature adaptive tuning system 500 to provide wired or wireless communication capabilities with other devices and cloud platforms. The tower group temperature adaptive adjustment system 500 may have access to a wireless network based on a communication standard, such as WiFi, 2G or 3G, or a combination thereof. In an exemplary embodiment, the communication component 515 receives a broadcast signal or broadcast related information from an external broadcast management system via a broadcast channel. In an exemplary embodiment, the communications component 515 further includes a Near Field Communication (NFC) module to facilitate short-range communications. For example, the NFC module may be implemented based on Radio Frequency Identification (RFID) technology, infrared data association (IrDA) technology, Ultra Wideband (UWB) technology, Bluetooth (BT) technology, and other technologies.

In an exemplary embodiment, the tower temperature adaptive adjustment system 500 may be implemented by one or more Application Specific Integrated Circuits (ASICs), Digital Signal Processors (DSPs), Digital Signal Processing Devices (DSPDs), Programmable Logic Devices (PLDs), Field Programmable Gate Arrays (FPGAs), controllers, micro-controllers, microprocessors, or other electronic components for performing the tower temperature adaptive adjustment method described above.

As will be appreciated by one skilled in the art, embodiments of the present application may be provided as a method, system, or computer program product. Accordingly, the present application may take the form of an entirely hardware embodiment, an entirely software embodiment or an embodiment combining software and hardware aspects. Furthermore, the present application may take the form of a computer program product embodied on one or more computer-usable storage media (including, but not limited to, disk storage, optical storage, and the like) having computer-usable program code embodied therein.

The present application is described with reference to flowchart illustrations and/or block diagrams of methods, apparatus (systems), and computer program products according to embodiments of the application. It will be understood that each flow and/or block of the flow diagrams and/or block diagrams, and combinations of flows and/or blocks in the flow diagrams and/or block diagrams, can be implemented by computer program instructions. These computer program instructions may be provided to a processor of a general purpose computer, special purpose computer, embedded processor, or other programmable data processing apparatus to produce a machine, such that the instructions, which execute via the processor of the computer or other programmable data processing apparatus, create means for implementing the functions specified in the flowchart flow or flows and/or block diagram block or blocks.

These computer program instructions may also be stored in a computer-readable memory that can direct a computer or other programmable data processing apparatus to function in a particular manner, such that the instructions stored in the computer-readable memory produce an article of manufacture including instruction means which implement the function specified in the flowchart flow or flows and/or block diagram block or blocks.

These computer program instructions may also be loaded onto a computer or other programmable data processing apparatus to cause a series of operational steps to be performed on the computer or other programmable apparatus to produce a computer implemented process such that the instructions which execute on the computer or other programmable apparatus provide steps for implementing the functions specified in the flowchart flow or flows and/or block diagram block or blocks.

It will be apparent to those skilled in the art that various changes and modifications may be made in the present application without departing from the spirit and scope of the application. Thus, if such modifications and variations of the present application fall within the scope of the claims of the present application and their equivalents, the present application is intended to include such modifications and variations as well.

Claims

1. A tower group temperature self-adaptive adjusting method is characterized by comprising the following steps:

in the operation process of the tower group, determining the feeding flow of each tower in the tower group according to the PID control action change value of the upper tower, the feedforward action change value of the upper tower, the feedback action change value of the lower tower and the original feeding flow of each tower in the tower group;

judging whether a first target tower with changed feeding flow exists or not;

when a first target tower with changed feeding flow exists, determining the temperature corresponding to the first target tower according to the changed feeding flow, the feeding flow before the change and a tower temperature set value before the change of the feeding flow;

2. The method of claim 1, further comprising:

determining the real-time liquid level control importance of each tower in the group according to the liquid level information;

3. The method of claim 2, wherein determining real-time liquid level control importance for each column in the group based on the liquid level information comprises:

determining the importance degree Ia of each tower;

determining the control importance degree Is of the liquid level of each tower;

4. A method according to claim 3, wherein said determining the degree of importance Ia for each column comprises:

if L is more than or equal to Lmax, Ia is 3+ (L-Lmax) 100/5;

if L is less than or equal to Lmin, Ia is 3+ (Lmin-L) 100/5;

t＝(Lr*V)/(Fout-Fin*α_btm)；

lr was calculated as follows: if Lr > (Lmax + Lmin)/2, then Lr is L-Lmax; if Lr is less than or equal to (Lmax + Lmin)/2, then Lr is L-Lmin.

5. The method of claim 3, wherein said determining a control importance Is for each column level comprises:

acquiring the control importance degree Is of the liquid level of each tower determined by the fuzzy controller based on the real quantity value;

6. The method as claimed in claim 3, wherein the determining the importance of control of the liquid level of each column I based on the importance of each column Ia and the importance of control of the liquid level of each column Is comprises:

I＝0.4Ia+0.1Is；

7. The method of claim 1 wherein determining the feed flow rates to each column in the stack based on the PID control action change value for the upper column, the feed forward action change value for the upper column, the feedback action change value for the lower column, and the raw feed flow rates to each column in the stack comprises:

the feed flow to each column in the column train is determined by the following equation:

Fin＝Pb+Qb+Fm+F0；

wherein Fin is the feed flow of each tower; pb is a change value of the PID control action of the upper tower; qb is the feed-forward action change value of the upper tower; fm is a lower tower feedback effect change value; f0 is the raw feed flow rate of each column.

8. The method of claim 1, wherein determining the temperature corresponding to the first target column based on the changed feed flow rate, the feed flow rate before the change, and the column temperature set point before the change in the feed flow rate comprises:

T＝K(F _{_feed2} -F_ _feed1 )+Tlast；

wherein T is a temperature determined according to the feed flow rate; k is the temperature corresponding coefficient of the feeding tower; f _ feed1 is an initial value of the feed flow within a preset sampling time; f _ feed2 is the final value of the feed flow within the preset sampling time; tlast is the column temperature set point at feed flow rate F feed 1.

9. A tower temperature adaptive adjustment system is characterized by comprising:

at least one processor; and the number of the first and second groups,

a memory communicatively coupled to the at least one processor; wherein,

the memory stores instructions executable by the one processor to perform the method of any one of claims 1-8 by the at least one processor.

10. A computer-readable storage medium, wherein instructions in the storage medium, when executed by a processor corresponding to the tower group temperature adaptive adjustment system, enable the tower group temperature adaptive adjustment system to implement the method of any one of claims 1-8.